Support properties of silica supported catalysts and their use in olefin metathesis

ABSTRACT

Silica supports having a surface area from about 250 m 2 /g to about 600 m 2 /g and an average pore diameter from about 45 Å to about 170 Å, used for supported tungsten catalysts, improves the activity of the resulting catalyst (i.e., its conversion level at a given temperature) for the metathesis of olefins, without compromising its selectivity to the desired conversion product(s). Exemplary catalysts and processes include those for the production of valuable light olefins such as propylene from a hydrocarbon feedstock comprising ethylene and butylene.

FIELD OF THE INVENTION

The invention relates to catalysts and processes for the metathesis ofolefins, for example in the production of propylene from olefinfeedstocks comprising ethylene and butylene. A representative catalystcomprises tungsten (e.g., present as tungsten oxide (WO₃)) on a supportcomprising silica having a surface area from about 250 m²/g to about 600m²/g and an average pore diameter from about 45 Å to about 170 Å.

DESCRIPTION OF RELATED ART

Propylene demand in the petrochemical industry has grown substantially,largely due to its use as a precursor in the production of polypropylenefor packaging materials and other commercial products. Other downstreamuses of propylene include the manufacture of acrylonitrile, acrylicacid, acrolein, propylene oxide and glycols, plasticizer oxo alcohols,cumene, isopropyl alcohol, and acetone. Currently, the majority ofpropylene is produced during the steam cracking or pyrolysis ofhydrocarbon feedstocks such as natural gas, petroleum liquids, andcarbonaceous materials (e.g., coal, recycled plastics, and organicmaterials). The major product of steam cracking, however, is generallyethylene and not propylene.

Steam cracking involves a very complex combination of reaction and gasrecovery systems. Feedstock is charged to a thermal cracking zone in thepresence of steam at effective conditions to produce a pyrolysis reactoreffluent gas mixture. The mixture is then stabilized and separated intopurified components through a sequence of cryogenic and conventionalfractionation steps. Generally, the product ethylene is recovered as alow boiling fraction, such as an overhead stream, from anethylene/ethane splitter column requiring a large number of theoreticalstages due to the similar relative volatilities of the ethylene andethane being separated. Ethylene and propylene yields from steamcracking and other processes may be improved using known methods for themetathesis or disproportionation of C₄ and heavier olefins, incombination with a cracking step in the presence of a zeolitic catalyst,as described, for example, in U.S. Pat. No. 5,026,935 and U.S. Pat. No.5,026,936. The cracking of olefins in hydrocarbon feedstocks, to producethese lighter olefins from C₄ mixtures obtained in refineries and steamcracking units, is described in U.S. Pat. Nos. 6,858,133; 7,087,155; and7,375,257.

Steam cracking, whether or not combined with conventional metathesisand/or olefin cracking steps, does not yield sufficient propylene tosatisfy worldwide demand. Other significant sources of propylene aretherefore required. These sources include byproducts of fluid catalyticcracking (FCC) and resid fluid catalytic cracking (RFCC), normallytargeting gasoline production. FCC is described, for example, in U.S.Pat. No. 4,288,688 and elsewhere. A mixed, olefinic C₃/C₄ byproductstream of FCC may be purified in propylene to polymer gradespecifications by the separation of C₄ hydrocarbons, propane, ethane,and other compounds.

Much of the current propylene production is therefore not “on purpose,”but as a byproduct of ethylene and gasoline production. This leads todifficulties in coupling propylene production capacity with its demandin the marketplace. Moreover, much of the new steam cracking capacitywill be based on using ethane as a feedstock, which typically producesonly ethylene as a final product. Although some hydrocarbons heavierthan ethylene are present, they are generally not produced in quantitiessufficient to allow for their recovery in an economical manner. In viewof the current high growth rate of propylene demand, this reducedquantity of co-produced propylene from steam cracking will only serve toaccelerate the increase in propylene demand and value in themarketplace.

A dedicated route to light olefins including propylene is paraffindehydrogenation, as described in U.S. Pat. No. 3,978,150 and elsewhere.However, the significant capital cost of a propane dehydrogenation plantis normally justified only in cases of large-scale propylene productionunits (e.g., typically 250,000 metric tons per year or more). Thesubstantial supply of propane feedstock required to maintain thiscapacity is typically available from propane-rich liquefied petroleumgas (LPG) streams from gas plant sources. Other processes for thetargeted production of light olefins involve high severity catalyticcracking of naphtha and other hydrocarbon fractions. A catalytic naphthacracking process of commercial importance is described in U.S. Pat. No.6,867,341.

More recently, the desire for propylene and other light olefins fromalternative, non-petroleum based feeds has led to the use of oxygenatessuch as alcohols and, more particularly, methanol, ethanol, and higheralcohols or their derivatives. Methanol, in particular, is useful in amethanol-to-olefin (MTO) conversion process described, for example, inU.S. Pat. No. 5,914,433. The yield of light olefins from such processesmay be improved using olefin cracking to convert some or all of the C₄ ⁺product of MTO in an olefin cracking reactor, as described in U.S. Pat.No. 7,268,265. An oxygenate to light olefins conversion process in whichthe yield of propylene is increased through the use of dimerization ofethylene and metathesis of ethylene and butylene, both products of theconversion process, is described in U.S. Pat. No. 7,586,018.

Despite the use of various dedicated and non-dedicated routes forgenerating light olefins industrially, the demand for propylenecontinues to outpace the capacity of such conventional processes.Moreover, further demand growth for propylene is expected. A needtherefore exists for cost-effective methods that can increase propyleneyields from both existing refinery hydrocarbons based on crude oil aswell as non-petroleum derived feed sources.

SUMMARY OF THE INVENTION

The invention is associated with the discovery of catalysts andprocesses for olefin metathesis, including those for the production ofvaluable light olefins such as propylene. More particularly, it has beenfound that a combination of properties of silica, and in particular asurface area and an average pore diameter (or pore size) within certainranges, when used for supported tungsten oxide catalysts, effectivelyimproves the activity of the resulting catalyst (i.e., its conversionlevel at a given temperature) for the metathesis of olefins, withoutsignificantly compromising its selectivity to the desired conversionproduct(s). In fact, the use of silica supports having the propertiesdescribed herein can surprisingly provide increases in both conversionand selectivity under favorable olefin metathesis conditions, contraryto normal expectations that greater conversion levels are obtained atthe expense of a loss in selectivity. The ranges of surface area andaverage pore diameter characteristics of silica, used in the tungstenoxide catalysts found to exhibit these performance advantages, are bothselected from much broader ranges representative of the wide variety ofsilicas (e.g., both amorphous and crystalline) available.

Without being bound by theory, it is thought that these experimentallyobserved benefits result from a synergistic combination of surface areaand average pore diameter, when within the ranges discussed herein, thatprovides favorable effects in terms of both reaction kinetics andmolecular diffusion. These effects are believed to contribute to thedemonstrated high yield (the product of conversion and selectivity) ofthe desired product(s). Increased olefin metathesis catalyst activitymay be exploited commercially by reducing the requirement to heat theolefin-containing hydrocarbon feedstock, prior to its contact with thecatalyst at the inlet of the olefin metathesis reaction zone.Alternatively, increased product yield may be obtained at a givenreactor temperature. It will be recognized that cost advantages,associated with decreased energy requirements and/or greater productvalue, result in either case. In view of the current demand forpropylene, it will also be appreciated that even a slight improvement inproduct yield, on the order of only a few percent, can result insubstantial economic advantages, on the order of several million dollarsper year in increased product value, for a typical petrochemicalproducer. The improved value of the product slate is accompanied by areduction in downstream separation requirements for removingnon-selective reaction products (e.g., C₅ ⁺ olefins), and also areduction in equipment and utilities required for the recycle ofunconverted olefin reactants.

Accordingly, embodiments of the invention relate to olefin metathesisprocesses comprising contacting a hydrocarbon feedstock with a catalystcomprising tungsten disposed on a support comprising silica having asurface area from about 250 m²/g to about 600 m²/g and an average porediameter from about 45 Å to about 170 Å. The hydrocarbon feedstockcomprises olefins including a first olefin (e.g., ethylene) and a secondolefin (e.g., butylene) having a carbon number of at least two greaterthan that of the first olefin, to produce a third olefin (e.g.,propylene) having a carbon number intermediate to the first and secondolefins. More particular embodiments of the invention relate toprocesses for producing propylene from the metathesis of ethylene andbutylene. The processes comprise contacting a hydrocarbon feedstockcomprising predominantly ethylene and butylene at an ethylene:butylenemolar ratio from about 0.5:1 to about 3:1 with a catalyst comprisingtungsten disposed on a silica support having a having a surface areafrom about 250 m²/g to about 600 m²/g and an average pore diameter fromabout 45 Å to about 170 Å. According to any of the above embodiments,the catalyst may comprise tungsten in an amount from about 1% to about10% by weight and the support may have a silica to alumina (SiO₂/Al₂O₃)molar ratio of at least about 1000. A representative conversion level ofthe ethylene and the butylene is from about 30% to about 80%, based oncarbon. Also, a representative selectivity, at which the ethylene andthe butylene are converted to propylene, is at least about 50%, based oncarbon.

Further embodiments of the invention relate to catalysts (e.g., forolefin metathesis) comprising tungsten (e.g., as tungsten oxide)disposed on a support comprising silica having a surface area from about250 m²/g to about 600 m²/g and an average pore diameter from about 45 Åto about 170 Å.

Yet further embodiments of the invention relate to methods for preparingcatalysts (e.g., for olefin metathesis) comprising tungsten oxidedisposed on a support comprising silica. The methods comprise (a)impregnating a support comprising silica having a surface area fromabout 250 m²/g to about 600 m²/g and an average pore diameter from about45 Å to about 170 Å with a tungsten compound to provide a tungstenimpregnated silica support, and (b) calcining the tungsten impregnatedsilica support to provide the catalyst.

These and other aspects and embodiments associated with the presentinvention are apparent from the following Detailed Description.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 graphically depicts the propylene yield obtained from themetathesis of ethylene and butylene at constant process conditions, inthe presence of catalysts comprising tungsten disposed on silicasupports, as a function of the surface area of the silica used in thesupports.

FIG. 2 graphically depicts product selectivity as a function of ethyleneand butylene conversion, at three different catalyst bed temperatures,namely 343° C. (649° F.), 400° C. (752° F.), and 425° C. (797° F.), inthe production of propylene from ethylene and butylene by olefinmetathesis in the presence of catalysts comprising tungsten disposed onsilica supports. The selectivity of the main product, propylene, as wellas the 5-carbon number and higher byproducts (C₅ ⁺) are both shown, asobtained using catalysts having supports containing silica with 3different average pore sizes.

FIG. 3 graphically depicts conversion of ethylene and propylene as afunction of time on stream in the production of propylene from ethyleneand butylene by olefin metathesis in the presence of catalystscomprising tungsten disposed on silica supports. The conversion datawere obtained using catalysts having supports containing silica with 3different average pore sizes.

FIG. 4 graphically depicts product selectivity as a function of ethyleneand butylene conversion, in the production of propylene from ethyleneand butylene by olefin metathesis in the presence of catalystscomprising tungsten, at four different tungsten levels, namely 1.5%, 4%,6.5%, and 9%, disposed on silica supports. The selectivity of the mainproduct, propylene, as well as the 5-carbon number and higher byproducts(C₅ ⁺) are both shown, as obtained using catalysts having supportscontaining silica with 3 different average pore sizes.

DETAILED DESCRIPTION

As discussed above, the present invention is associated with catalyticolefin metathesis (or disproportionation) processes in which ahydrocarbon feedstock is contacted, in a metathesis reactor or reactionzone, with a catalyst comprising tungsten disposed on a supportcomprising silica having properties found to be particularlyadvantageous, including a surface area from about 250 m²/g to about 600m²/g and an average pore diameter from about 45 Å to about 170 Å. Thehydrocarbon feedstock refers to the total, combined feed, including anyrecycle hydrocarbon streams, to the catalyst in the metathesis reactoror reaction zone, but not including any non-hydrocarbon gaseous diluents(e.g., nitrogen), which may be added along with the feed according tosome embodiments. The hydrocarbon feedstock may, but does notnecessarily, comprise only hydrocarbons. The hydrocarbon feedstockgenerally comprises predominantly (i.e., at least 50% by weight)hydrocarbons, typically comprises at least about 80% (e.g., from about80% to about 100%) hydrocarbons, and often comprises at least about 90%(e.g., from about 90% to about 100% by weight) hydrocarbons.

Also, in olefin metathesis processes according to the present invention,the hydrocarbons contained in the hydrocarbon feedstock are generallypredominantly (i.e., at least 50% by weight, such as from about 60% toabout 100% by weight) olefins, typically they comprise at least about75% (e.g., from about 75% to about 100%) by weight olefins, and oftenthey comprise at least about 85% (e.g., from about 85% to about 100% orfrom about 95% to about 100%) by weight olefins. In other embodiments,these amounts of olefins are representative of the total olefinpercentages in the hydrocarbon feedstock itself, rather than the olefinpercentages of the hydrocarbons in the hydrocarbon feedstock. In yetfurther embodiments, these amounts of olefins are representative of thetotal percentage of two particular olefins in the hydrocarbon feedstock,having differing carbon numbers, which can combine in the metathesisreactor or reaction zone to produce a third olefin having anintermediate carbon number (i.e., having a carbon number intermediate tothat of (i) a first olefin (or first olefin reactant) and (ii) a secondolefin (or second olefin reactant) having a carbon number of at leasttwo greater than that of the first olefin). In general, the two olefinsare present in the hydrocarbon feedstock to the metathesis reactor in amolar ratio of the first olefin to the second olefin from about 0.2:1 toabout 10:1, typically from about 0.5:1 to about 3:1, and often fromabout 1:1 to about 2:1.

In an exemplary embodiment, the two olefins (first and second olefins)of interest are ethylene (having two carbons) and butylene (having fourcarbons), which combine in the metathesis reactor or reaction zone toproduce desired propylene (having three carbons). The term “butylene” ismeant to encompass the various isomers of the C₄ olefin butene, namelybutene-1, cis-butene-2, trans-butene-2, and isobutene. In the case ofmetathesis reactions involving butylene, it is preferred that thebutylene comprises predominantly (i.e., greater than about 50% byweight) butene-2 (both cis and trans isomers) and typically comprises atleast about 85% (e.g., from about 85% to about 100%) butene-2, asbutene-2 is generally more selectively converted, relative to butene-1and isobutylene, to the desired product (e.g., propylene) in themetathesis reactor or reaction zone. In some cases, it may be desirableto increase the butene-2 content of butylene, for example to achievethese ranges, by subjecting butylene to isomerization to convertbutene-1 and isobutylene, contained in the butylene, to additionalbutene-2. The isomerization may be performed in a reactor that isseparate from the reactor used for olefin metathesis. Alternatively, theisomerization may be performed in an isomerization reaction zone in thesame reactor that contains an olefin metathesis reaction zone, forexample by incorporating an isomerization catalyst upstream of theolefin metathesis catalyst or even by combining the two catalysts in asingle catalyst bed. Suitable catalysts for carrying out the desiredisomerization to increase the content of butene-2 in the butylene areknown in the art and include, for example, magnesium oxide containingisomerization catalysts as described in U.S. Pat. No. 4,217,244.

As discussed above, the olefins may be derived from petroleum ornon-petroleum sources. Crude oil refining operations yielding olefins,and particularly butylene, include hydrocarbon cracking processescarried out in the substantial absence of hydrogen, such as fluidcatalytic cracking (FCC) and resid catalytic cracking (RCC). Olefinssuch as ethylene and butylene are recovered in enriched concentrationsfrom known separations, including fractionation, of the total reactoreffluents from these processes. Another significant source of ethyleneis steam cracking, as discussed above. A stream enriched in ethylene isgenerally recovered from an ethylene/ethane splitter as a low boilingfraction, relative to the feed to the splitter, which fractionates atleast some of the total effluent from the steam cracker and/or otherethylene containing streams. In the case of olefins derived fromnon-petroleum sources, both the ethylene and butylene, for example, maybe obtained as products of an oxygenate to olefins conversion process,and particularly a methanol to light olefins conversion process. Suchprocesses are known in the art, as discussed above, and optionallyinclude additional conversion steps to increase the butylene yield suchas by dimerization of ethylene and/or selective saturation of butadiene,as described in U.S. Pat. No. 7,568,018. According to variousembodiments of the invention, therefore, at least a portion of theethylene in the hydrocarbon feedstock is obtained from a low boilingfraction of an ethylene/ethane splitter and/or at least a portion of thebutylene is obtained from an oxygenate to olefins conversion process.

In representative olefin metathesis processes, with an exemplary processbeing the metathesis of ethylene and butylene for the production ofpropylene, catalysts comprising tungsten (e.g., as tungsten oxide priorto use in olefin metathesis) supported on silica having the advantageousproperties described herein, may be used to achieve economicallyfavorable product yields under commercial process conditions. Withrespect to the first and second olefins (e.g., ethylene and butylene)that undergo metathesis, the conversion level, based on the amount ofcarbon in these reactants that are converted to the desired product andbyproducts (e.g., propylene and heavier, C₅ ⁺ hydrocarbons), isgenerally from about 40% to about 80% by weight, and typically fromabout 50% to about 75% by weight. Significantly higher conversionlevels, on a “per pass” basis through the metathesis reactor or reactionzone, are normally difficult to achieve due to equilibrium limitations,with the maximum conversion depending on the specific olefin reactantsand their concentrations as well as process conditions (e.g.,temperature).

In one or more separations (e.g., fractionation) downstream of themetathesis reactor or reaction zone, the desired product (e.g.,propylene) may be recovered in substantially pure form by removing andrecovering unconverted olefins (e.g., ethylene and butylene) as well asreaction byproducts (e.g., C₅ ⁺ hydrocarbons including olefin oligomersand alkylbenzenes). Recycling of the unconverted olefin reactants backto the metathesis reactor or reaction zone may often be desirable forachieving complete or substantially complete overall conversion, or atleast significantly higher overall conversion (e.g., from about 80% toabout 100% by weight, or from about 95% to about 100% by weight) thanthe equilibrium-limited per pass conversion levels discussed above. Thedownstream separation(s) are normally carried out to achieve a highpurity of the desired product, particularly in the case of propylene.For example, the propylene product typically has a purity of at leastabout 99% by volume, and often at least about 99.5% by volume to meetpolymer grade specifications. According to other embodiments, thepropylene purity may be lower, depending on the end use of this product.For example, a purity of at least about 95% (e.g., in the range fromabout 95% to about 99%) by volume may be acceptable for a non-polymertechnology such as acrylonitrile production, or otherwise forpolypropylene production processes that can accommodate a lower puritypropylene.

At the per pass conversion levels discussed above, the selectivity ofthe converted feedstock olefin components (e.g., ethylene and propylene)to the desired olefin(s) (e.g., propylene) having an intermediate carbonnumber is generally at least about 75% (e.g., in the range from about75% to about 100%) by weight, typically at least about 80% (e.g., in therange from about 80% to about 99%) by weight, and often at least about90% (e.g., in the range from about 90% to about 97%) by weight, based onthe amount of carbon in the converted products. The per pass yield ofthe desired olefin(s) is the product of the selectivity to this/theseproduct(s) and the per pass conversion, which may be within the rangesdiscussed above. The overall yield, using separation and recycle of theunconverted olefin reactants as discussed above, can approach this/theseproduct selectivity/selectivities, as essentially complete conversion isobtained (minus some purge and solution losses of feedstock andproduct(s), as well as losses due to downstream separationinefficiencies).

The conversion and selectivity values discussed above are achieved bycontacting the hydrocarbon feedstock described above, eithercontinuously or batchwise, with a catalyst as described hereincomprising tungsten disposed on a support comprising silica having asurface area from about 250 m²/g to about 600 m²/g and an average porediameter from about 45 Å to about 170 Å. Generally, the contacting isperformed with the hydrocarbon feedstock being passed continuouslythrough a fixed bed of the catalyst in an olefin metathesis reactor orreaction zone. For example, a swing bed system may be utilized, in whichthe flowing hydrocarbon feedstock is periodically re-routed to (i)bypass a bed of catalyst that has become spent or deactivated and (ii)subsequently contact a bed of fresh catalyst. A number of other suitablesystems for carrying out the hydrocarbon/feedstock contacting are knownin the art, with the optimal choice depending on the particularfeedstock, rate of catalyst deactivation, and other factors. Suchsystems include moving bed systems (e.g., counter-current flow systems,radial flow systems, etc.) and fluidized bed systems, any of which maybe integrated with continuous catalyst regeneration, as is known in theart.

As discussed above, the use of silica having a surface area from about250 m²/g to about 600 m²/g and an average pore diameter from about 45 Åto about 170 Å, as a support for the olefin metathesis catalystcomprising tungsten, results in significant performance benefits interms of both catalyst activity and selectivity, and consequently theyield of the desired product (e.g., propylene) achieved at a givenreaction temperature. Surprisingly, therefore, the increase inconversion level does not result in a loss in selectivity, as isnormally observed, for example, when reaction severity is increased(e.g., by raising temperature, increasing residence time, and/orincreasing reactant concentrations). Representative conditions forolefin metathesis (i.e., conditions for contacting the hydrocarbonfeedstock and catalyst in the olefin metathesis reactor or reactionzone), in which the above conversion and selectivity levels may beobtained, include a temperature from about 300° C. (572° F.) to about600° C. (1112° F.), and often from about 400° C. (752° F.) to about 500°C. (932° F.); a pressure from about 10 barg (145 psig) to about 80 barg(1160 psig), and often from about 15 barg (218 psig) to about 45 barg(653 psig); and a weight hourly space velocity (WHSV) from about 1 hr⁻¹to about 10 hr⁻¹. As is understood in the art, the WHSV is the weightflow of the hydrocarbon feedstock divided by the weight of the catalystbed and represents the equivalent catalyst bed weights of feed processedevery hour. The WHSV is related to the inverse of the reactor residencetime. Under the olefin metathesis conditions described above, thehydrocarbon feedstock is normally in the vapor phase in the olefinmetathesis reactor or reaction zone, but it may also be in the liquidphase, for example, in the case of heavier (higher carbon number) olefinfeedstocks.

Importantly, the tungsten catalysts according to embodiments of theinvention and providing the significant benefits, as discussed herein,in olefin metathesis comprise a support comprising silica having theadvantageous properties described above. In general, the silica supportcomprises predominantly (i.e., at least 50% by weight) silica, with theoptional addition of other components such as other inorganic refractorymetal oxides (e.g., alumina, zirconia, titania, boria, thoria, ceria)and/or catalyst promoters or modifiers (e.g., alkali or alkaline earthmetals, or transition metals in addition to tungsten). Typically, thesupport comprises silica in an amount of at least about 90% (e.g., fromabout 90% to about 100%) by weight and often at least about 95% (e.g.,from about 95% to about 100%) by weight.

Types of silica for use as a component of, or otherwise for all orsubstantially all of, the silica support include amorphous silicas.Examples include Davisil®646, Davisil®636 (W.R. Grace & Co., Columbia,Md.) and other precipitated silicas. Regardless of the source, thesilica will have a surface area, either as received or after an optionalacid washing step in the catalyst preparation procedure, of at leastabout 250 square meters per gram (m²/g), with particularly advantageousresults being obtained in the range from about 250 m²/g to about 600m²/g, and often from about 400 m²/g to about 550 m²/g. The average porediameter of the silica, either as received or after acid washing, ispreferably at least about 40 angstoms (Å), with exemplary average porediameters being in the range from about 45 Å to about 170 Å, and even inthe range from about 45 Å to about 100 Å. Surface area and average porediameter are measured according to the Brunauer, Emmett and Teller (BET)method based on nitrogen adsorption (ASTM D1993-03(2008)). As discussedabove, it is thought that the combination of surface area and averagepore diameter characteristics act in synergy, in the catalysts forolefin metathesis as described herein, to provide highly effectivekinetic and size selective properties that simultaneously benefit bothconversion and product selectivity.

Crystalline silicas may also be used in the silica support, withmesoporous materials such as MCM-41 being representative. Exemplarycrystalline silicas have a silica to alumina molar ratio of at leastabout 1,000 corresponding to an atomic silicon to aluminum ratio (Si:Alratio) of at least about 500. Typically, such siliceous materials usedin the silica support have a silica to alumina molar ratio of at leastabout 3,000 (e.g., from about 3,000 to about 15,000), and often at leastabout 5,000 (e.g., from about 5,000 to about 10,000).

The silica support and consequently the catalyst itself can have anumber of possible physical forms, with the specific form usuallydepending principally on the particular reaction system used. Thesupport may be, for example, in the form of a powder that is sized to adesired average particle size, for example from about 35 mesh (0.50 mm)to about 60 mesh (0.25 mm). In reaction systems where a powder formwould lead to an undesirably high pressure drop, larger spheres orextrudates (e.g., in the form of elongated cylinders) are commonlyemployed, with the specific shape being determined by factors such aspressure drop, mobility, diffusional distance, etc. In representativeembodiments, the support has an average particle size, based on arepresentative dimension of the particle form (e.g., the diameter of aspherical form or the diameter of the circular cross section of acylindrical, extruded form) from about 0.1 mm to about 5 mm.

In the preparation of catalysts for olefin metathesis, a supportcomprising silica having the properties described herein is impregnatedwith a tungsten compound to provide a tungsten impregnated silicasupport. Impregnation generally involves contacting the support with animpregnation solution of the tungsten compound. Suitable compoundsinclude ammonium tungstate compounds such as ammonium metatungstate(AMT) and ammonium paratungstate (APT). The concentration of thetungsten compound in such impregnation solutions generally ranges fromabout 0.1 M to about 5 M. Static or flowing conditions may be used forcontacting between the impregnation solution and silica support toeffect the desired degree of tungsten impregnation. The impregnationsolution contacting temperature is generally in the ranges from about20° C. (68° F.) to about 200° C. (392° F.), and often from about 25° C.(77° F.) to about 150° C. (302° F.). The duration of contacting at thistemperature (or contacting time) is generally from about 1 minute toabout 5 hours, and often from about 5 minutes to about 3 hours. Thecontacting time is inclusive of any subsequent drying step, in which thesupport and impregnation solution remain in contact at a temperaturewithin these ranges. The impregnation conditions are selected to achievea desired level of tungsten (as tungsten metal), for example from about1% to about 10% by weight, in the resulting catalyst.

Following impregnation, the tungsten impregnated support is thencalcined to convert the tungsten compound to tungsten oxide (WO₃) thatis a stable form of the tungsten prior to use, for example, in olefinmetathesis. Calcining procedures that are effective for converting allor substantially all of the tungsten compound to WO₃ generally involveheating the support after impregnation to a temperature from about 300°C. (572° F.) to about 750° C. (1382° F.), and often from about 400° C.(752° F.) to about 650° C. (1202° F.), for a time (or duration ofheating or the support to this temperature) generally from about 1 hourto about 10 hours, and often from about 3 hours to about 9 hours. Theheating is normally performed with a flow of oxygen-containing gas(e.g., air, oxygen, or oxygen-enriched air). Usually during the catalystpreparation procedure, drying of the impregnated silica support isperformed after the impregnation and before calcining of the tungstenimpregnated silica support. Typical conditions for this drying step, ifused, include a temperature from about 25° C. (77° F.) to about 250° C.(482° F.) and a time from about 0.5 hours to about 24 hours. The dryingand/or calcining steps may be performed under purge with a gas (e.g.,air, oxygen, nitrogen, argon, etc. or mixture of gases), preferably atambient or slightly elevated pressure.

After calcination, it is possible to convert the tungsten oxide to othertungsten forms, for example by partial or complete reduction in thepresence of flowing hydrogen, which may be more desirable within thereaction environment for catalyzing a particular reaction. Theconversion may occur, for example, shortly prior to use and even in situas a catalyst pretreatment. Therefore, while the catalyst may beprepared with the tungsten as tungsten oxide on a support comprisingsilica, it is not necessary that the tungsten oxide form be conserved inthe reaction environment.

Optionally, acid washing of the silica support having the propertiesdescribed herein and found to result in significant advantages withrespect to tungsten catalysts for olefin metathesis, may be carried outprior to impregnation with the tungsten compound. Acid washing involvescontacting the silica used in the support with an acid, including anorganic acid or an inorganic acid. Particular inorganic acids includenitric acid, sulfuric acid, and hydrochloric acid, with nitric acid andhydrochloric acid being preferred. The acid concentration in aqueoussolution, used for the acid washing, is generally in the range fromabout 0.05 molar (M) to about 3 M, and often from about 0.1 M to about 1M. The acid washing can be performed under static conditions (e.g.,batch) or flowing conditions (e.g., once-through, recycle, or with acombined flow of make-up and recycle solution).

Representative contacting conditions used to provide an acid washedsilica support include a temperature generally from about 20° C. (68°F.) to about 120° C. (248° F.), typically from about 30° C. (86° F.) toabout 100° C. (212° F.), and often from about 50° C. (122° F.) to about90° C. (194° F.). The contacting time, or a duration over which thesilica support is contacted with the acid at a temperature within any ofthese ranges, is generally from about from about 10 minutes to about 5hours, and often from about 30 minutes to about 3 hours. Normally, it ispreferred that the conditions of contacting used to perform acid washingof the silica support result in one or more observed physical orcompositional changes in the support that can be verified analytically.For example, it has been determined that effective acid washing isgenerally accompanied by an increase in the surface area (BET method asindicated above) of the silica support of at least 5% (e.g., from about5% to about 20%), and often at least 10% (e.g., from about 10% to about15%), relative to the surface area of the support prior to being acidwashed. Another change is a decrease in the amount of aluminum (asaluminum metal) of the acid washed support, relative to the amount inthe support prior to being acid washed. The reduction in aluminum can beverified using inductively coupled plasma (ICP) techniques, known in theart, for the determination of trace metals. Generally, the amount ofaluminum is decreased by at least about 35% (e.g., from about 35% toabout 90%) and often at least about 50% (e.g., from about 50% to about80%). A third change is a decrease in the average pore diameter of theacid washed silica support, relative to the average pore diameter of thesupport prior to being acid washed. In general, the pore volume isdecreased by at least about 5%, and often by at least about 10%.

Overall aspects of the invention are directed to catalysts, andassociated olefin metathesis processes, that exploit the significantbenefits associated supports comprising silica having a surface areafrom about 250 m²/g to about 600 m²/g and an average pore diameter fromabout 45 Å to about 170 Å. Those having skill in the art, with theknowledge gained from the present disclosure, will recognize thatvarious changes can be made in the above catalysts, processes using thecatalysts, and methods of making the catalysts, without departing fromthe scope of the present disclosure.

The following examples are representative of the present invention andits associated advantages and are not to be construed as limiting thescope of the invention as set forth in the appended claims.

EXAMPLE 1

Characterization of Silica Supports

Samples of 6 different silicas were obtained as silica powders fromcommercial sources. These silicas were the mesoporous molecular sieveMCM-41 (Mobil Composition of Matter No. 41, available fromSigma-Aldrich, Inc., St. Louis, Mo., USA) and the precipitated silicas(available from W.R. Grace & Co., Columbia, Md.) having the tradenamesDavisil®12, Davisil®923, Davisil®636, Davisil®646, and GraceXWP-Gel-P005 (extra wide pore silica). The silica samples were analyzedfor surface area and average pore diameter using the BET methoddescribed above, and this analysis revealed a wide range in bothparameters for commercial silica samples, as shown below in Table 1.

TABLE 1 Surface Areas and Average Pore Diameters of Silicas XWP-Davisil ® Davisil ® Davisil ® Gel- Davisil ® MCM- 923 636 646 P005 12 41BET 484 451 293 80 691 974 Sur- face Area, m²/g Pore 32 78 166 430 23 36Di- am- eter, Å

EXAMPLE 2

Tungsten Impregnation of Silica Supports and Calcination

Each of the 6 different silica samples described in Example 1, sized to35-60 US mesh (0.25-0.5 mm), was impregnated with tungsten. Theimpregnation was performed at varying targeted tungsten levels, namely1.5%, 4%, 6.5%, and 9% (as tungsten metal) based on the total drycatalyst weight. To perform the impregnation, the supports were weighedinto 12 crucibles using about 1-2 ml per crucible well. Weighing wasperformed either manually or otherwise using an automated powderdispensing system. The tungsten was added, in the form of an ammoniummetatungstate solution, to separate empty crucibles. Liquid reagent waspipetted and diluted with deionized water, to obtain about a 2:1solution to silica ratio, using the Zinsser Lissy® GXL liquid handlingsystem. The solids were then added to the corresponding liquids. Themixtures were placed on a vortexer for 10 minutes and then rotary driedunder 2 psig flowing nitrogen at 120° C. (248° F.) for 1-2 hours, untilfree flowing. The dried, tungsten impregnated silica supports were thencalcined in a muffle oven under low pressure air flow for one hour at100° C. (212° F.) and three hours at 500° C. (932° F.). The resultingtungsten oxide catalysts on silica supports were then evaluated fortheir performance in the metathesis of ethylene and butylene to producepropylene, as described below in Example 3.

EXAMPLE 3

Evaluation of Tungsten Oxide Catalysts

The WO₃ catalysts prepared in Example 2 were evaluated for metathesis ofan ethylene and butylene feedstock to produce propylene in ahigh-throughput experimental protocol. Samples of the catalysts, 200microliter (μl) each, were tested in a microreactor array system (HighPressure Reactor Assay Module from Sintef (Trondheim, Norway)) equippedwith a gas and liquid flow control module, reactor/oven assembly, andanalytical section providing 48 individual reactor channels. Thecatalysts were reduced for 45 minutes at 500° C. (932° F.) under flowinghydrogen, using a temperature ramp rate of 2° C. (4° F.) per minute. Thetests were performed at catalyst bed temperatures of 343° C. (649° F.),400° C. (752° F.), 425° C. (797° F.), and 343° C. (649° F.),respectively. The four temperature conditions were evaluatedconsecutively over durations of 4, 4, 6, and 4 hours, respectively.

A hydrocarbon feedstock of ethylene and butylene at an ethylene:butylenetarget molar ratio of 1.5 was supplied from cylinders, with the ethylenemeeting ultra high purity (UHP) specifications and the butylene beingtechnical grade material containing about 93-95 mole-% cis and trans2-butenes. The liquid hourly space velocity (LHSV), or volumetric flowrate of the hydrocarbon feedstock divided by the catalyst bed volume,was controlled at 0.9 hr⁻¹. Also, the reactor pressure set point wasmaintained at a target value of 32 barg (465 psig) throughout the olefinmetathesis testing.

The reactor effluent composition was analyzed periodically using ahigh-speed gas chromatography method developed to accommodate thehigh-throughput experimentation. The analytical results were used todetermine both the conversion level (per pass), based on the totalpercentage conversion of feed carbon, and the selectivity, based on thetotal percentage of converted carbon that resulted in the formation ofpropylene. Average propylene selectivity and feed conversion values (perpass) were calculated over the duration of each temperature conditionused for olefin metathesis performance evaluation. The propylene yield(per pass) was calculated as the product of conversion and selectivity.

FIG. 1 shows the propylene yield, at 425° C. (797° F.) reactortemperature, obtained from the olefin metathesis evaluation, as afunction of the BET surface area of the silica used in the catalystsupports. The other process conditions were as described above. The fivecatalysts compared in this figure had a target 6.5 wt-% tungsten loadingon Davisil®12, Davisil®923, Davisil®636, Davisil®646, and GraceXWP-Gel-P005 (extra wide pore silica). The results show that significantand commercially important advantages in terms of propylene yield areobtained for supports comprising silica having a BET surface area ofabout 450 m²/g and more broadly in the range from about 250 m²/g toabout 600 m²/g.

FIG. 2 shows the propylene selectivity, as well as the C₅ ⁺ hydrocarbonbyproduct selectivity, as a function of conversion obtained from theolefin metathesis evaluation at the three different catalyst bedtemperatures, namely 343° C. (649° F.), 400° C. (752° F.), and 425° C.(797° F.). The other process conditions were as described above. Thethree catalysts compared in this figure had a target 6.5 wt-% tungstenloading on Davisil®12, Davisil®923, and Davisil®636. The results showthat the catalyst supported on Davisil®636 had not only increasedactivity (conversion level at a given temperature) but also increasedpropylene selectivity and decreased C₅ ⁺ selectivity, compared tocatalysts having supports comprising silica with other surfacearea/average pore diameter characteristics. While the Davisil®923 silicahad a surface area in the range from about 250 m²/g to about 600 m²/g,the average pore diameter of the silica was below the range of 45 Å to170 Å, as discussed above. Davisil®12 did not have a surface area oraverage pore diameter within these desired ranges.

FIG. 3 shows conversion, at 425° C. (797° F.) catalyst bed temperatureas a function of time on stream, obtained from the olefin metathesisevaluation. The other process conditions were as described above. Theconversion data were obtained using catalysts having supports containingsilica with 3 different average pore sizes. The three catalysts comparedin this figure had a target 6.5 wt-% tungsten loading on Davisil®12,Davisil®923, and Davisil®636. Again, the results show the superiority inperformance of the catalyst supported on Davisil®636, compared tocatalysts having supports comprising silica with other surfacearea/average pore diameter characteristics.

FIG. 4 shows the propylene selectivity, as well as the C₅ ⁺ hydrocarbonbyproduct selectivity, as a function of conversion obtained from theolefin metathesis evaluation at 425° C. (797° F.) catalyst bedtemperature. The other process conditions were as described above. Thecatalysts compared in this figure had target tungsten loadings of 1.5wt-%, 4 wt-%, 6.5 wt-%, and 9 wt-% on three different silica types,namely Davisil®636, Davisil®646, and Grace XWP-Gel-P005 (extra wide poresilica). The results show the superiority in conversion and/orselectivity of the catalyst supported on Davisil®636 or Davisil®646silica, compared to catalysts having supports comprising silica withother surface area/average pore diameter characteristics. XWP-Gel-P005(extra wide pore silica) did not have a surface area or average porediameter within the desired ranges discussed above.

The above results illustrate that WO₃ catalysts having supportscomprising silica with the surface area/average pore diametercharacteristics described herein, provide exceptional performance inolefin metathesis.

1. An olefin metathesis process comprising: contacting a hydrocarbonfeedstock with a catalyst comprising tungsten disposed on a supportcomprising silica having a surface area from about 400 m²/g to about 550m²/g and an average pore diameter from about 45 Å to about 170 Å,wherein the hydrocarbon feedstock comprises olefins including a firstolefin and a second olefin having a carbon number of at least twogreater than that of the first olefin, to produce a third olefin havingan intermediate carbon number, wherein the first olefin is ethylene, thesecond olefin is butylene, and the third olefin is propylene.
 2. Theprocess of claim 1, wherein the hydrocarbon feedstock comprises at leastabout 85% by weight olefins.
 3. The process of claim 1, wherein a molarratio of the first olefin to the second olefin in the hydrocarbonfeedstock is from about 0.5:1 to about 3:1.
 4. The process of claim 1,wherein at least a portion of the ethylene is obtained from a lowboiling fraction of an ethylene/ethane splitter.
 5. The process of claim1, wherein at least a portion of the butylene is obtained from anoxygenate to olefins conversion process or a fluid catalytic crackingprocess.
 6. The process of claim 1, wherein the first olefin and thesecond olefin are converted to the third olefin with a selectivity of atleast about 80% by weight based on carbon in the converted products. 7.The process of claim 1, wherein the hydrocarbon feedstock is contactedwith the catalyst at a temperature from about 300° C. (572° F.) to about600° C. (1112° F.), a pressure from about 10 barg (145 psig) to about 80barg (1160 psig), and a weight hourly space velocity from about 1 hr⁻¹to about 10 hr⁻¹.